Catalyst and process for removing mercaptans from hydrocarbon streams
The invention relates to a catalyst for a process for removing mercaptans and optionally disulfides (if present) from hydrocarbon streams, in particular C4 streams, in the presence of higher dienes, in particular C5 dienes. At the same time, the invention also relates to a process for removing mercaptans and disulfides (if present) from hydrocarbon streams, in particular C4 streams, in one embodiment in the presence of 1-butene, by thioetherification of the mercaptans with polyunsaturated hydrocarbons, wherein the process is carried out in a reactor with addition of hydrogen in the presence of higher dienes, in particular C 5 dienes.
1. A heterogeneous catalyst for complete conversion of mercaptans from hydrocarbon streams comprising C2 to C8 olefins, wherein a heterogeneous catalyst comprises a support material and catalytically active metal and the heterogeneous catalyst is a shell catalyst,
and the support material is selected from the group consisting of alumina, silica gel and activated carbon and the catalytically active metals are palladium and platinum,
and the heterogeneous catalyst has a palladium concentration of up to 2.0% by weight, a platinum concentration of up to 1.0% by weight and a total metal dispersion of at least 70%, and
wherein the catalyst comprises an inner surface area of from 50 to 400 m 2 /g.
2. The heterogeneous catalyst according to claim 1 , wherein the palladium concentration of up to 1.0% by weight and the hydrocarbon streams comprising C3 to C6 olefins,
wherein the catalyst comprises an inner surface area of from 100 to 300 m 2 /g, and
wherein the heterogeneous catalyst has a total metal dispersion of at least 80%.
3. The heterogeneous catalyst according to claim 1 , wherein the platinum concentration of up to 0.5% by weight and the hydrocarbon streams comprise C4 olefins, and
wherein the catalyst comprises an inner surface area of from 200 to 300 m 2 /g.
4. The heterogeneous catalyst according to claim 1 , wherein the heterogeneous catalyst has a total metal surface area of at least 0.5 m 2 /g.
5. The heterogeneous catalyst according to claim 1 , wherein the heterogeneous catalyst has a total metal dispersion of at least 80%.
6. The heterogeneous catalyst according to claim 1 , wherein the palladium concentration of up to 0.5% by weight.
7. The heterogeneous catalyst according to claim 1 , wherein the platinum concentration of up to 0.2% by weight.
8. The heterogeneous catalyst according to claim 1 , wherein the heterogeneous catalyst has a total metal surface area of at least 1.0 m 2 /g.
9. A process for complete conversion of mercaptans from hydrocarbon streams in the presence of at least one higher diene by thioetherification of the mercaptans with polyunsaturated hydrocarbons, wherein the process is carried out in a reactor with addition of hydrogen, wherein the molar ratio of hydrogen to polyunsaturated hydrocarbons is not more than one, wherein a heterogeneous catalyst comprises a support material and a catalytically active metal used in the process comprises palladium and platinum as catalytically active metals, wherein the heterogeneous catalyst has a palladium concentration of up to 2.0% by weight, a platinum concentration of up to 1.0% by weight and a total metal dispersion of at least 70%.
10. The process according to claim 9 , wherein the higher diene is a C 5 diene.
11. The process according to claim 9 , wherein the mercaptans are thioetherified with polyunsaturated hydrocarbons, wherein the polyunsaturated hydrocarbons are selected from the group consisting of 1,3-butadiene, but-3-en-1-yne and 1,2-butadiene.
12. The process according to claim 9 , wherein at least ethanethiol and/or methanethiol are present as mercaptans.
13. The process according to claim 9 , wherein the molar ratio of hydrogen to polyunsaturated hydrocarbons is between 0.01 and 0.8.
14. The process according to claim 9 , wherein it is carried out in the presence of carbon monoxide, wherein the content of carbon monoxide in the reactor feed is less than 20 ppm based on the mass of the feed.
15. The process according to claim 9 , wherein the inlet temperature of the reactor feed is between 0° C. and 180° C.
16. The process according to claim 9 , wherein it is operated as a liquid-phase process and that the hydrogen is dissolved completely in the liquid phase.
17. The process according to claim 9 , wherein a C 4 hydrocarbon stream is used as feed for the reactor.
18. The process according to claim 9 , wherein, if 1-butene is present in the hydrocarbon stream in a concentration that is higher than the concentration at thermodynamic equilibrium for the double bond isomerization of 1-butene to 2-butene, the conversion of 1-butene into 2-butenes through isomerization and/or the hydrogenation to n-butane is less than 5%.
19. The process according to claim 9 , wherein the diene is a isoprene.
20. The process according to claim 9 , wherein the molar ratio of hydrogen to polyunsaturated hydrocarbons is between 0.1 and 0.5.